CN220012315U - Biochemical and ozone oxidation coupling reactor device - Google Patents
Biochemical and ozone oxidation coupling reactor device Download PDFInfo
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- CN220012315U CN220012315U CN202321468461.2U CN202321468461U CN220012315U CN 220012315 U CN220012315 U CN 220012315U CN 202321468461 U CN202321468461 U CN 202321468461U CN 220012315 U CN220012315 U CN 220012315U
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- ozone oxidation
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- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 title claims abstract description 130
- 238000007254 oxidation reaction Methods 0.000 title claims abstract description 82
- 230000003647 oxidation Effects 0.000 title claims abstract description 80
- 230000008878 coupling Effects 0.000 title claims abstract description 15
- 238000010168 coupling process Methods 0.000 title claims abstract description 15
- 238000005859 coupling reaction Methods 0.000 title claims abstract description 15
- 239000000945 filler Substances 0.000 claims abstract description 74
- 244000005700 microbiome Species 0.000 claims abstract description 58
- 238000001179 sorption measurement Methods 0.000 claims abstract description 29
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 29
- 238000005273 aeration Methods 0.000 claims abstract description 26
- 230000004060 metabolic process Effects 0.000 claims abstract description 26
- 238000005276 aerator Methods 0.000 claims description 25
- 238000012856 packing Methods 0.000 claims description 14
- 238000005192 partition Methods 0.000 claims description 13
- 238000006385 ozonation reaction Methods 0.000 claims description 4
- 239000007789 gas Substances 0.000 description 23
- 239000002351 wastewater Substances 0.000 description 22
- 238000000034 method Methods 0.000 description 11
- 230000008569 process Effects 0.000 description 9
- 239000003054 catalyst Substances 0.000 description 7
- 238000005265 energy consumption Methods 0.000 description 6
- 238000006243 chemical reaction Methods 0.000 description 5
- 239000010842 industrial wastewater Substances 0.000 description 5
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 4
- 238000005842 biochemical reaction Methods 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 239000001301 oxygen Substances 0.000 description 4
- 229910052760 oxygen Inorganic materials 0.000 description 4
- 230000005611 electricity Effects 0.000 description 3
- 230000009467 reduction Effects 0.000 description 3
- 230000009471 action Effects 0.000 description 2
- 230000015556 catabolic process Effects 0.000 description 2
- 238000006731 degradation reaction Methods 0.000 description 2
- 239000003344 environmental pollutant Substances 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 239000000178 monomer Substances 0.000 description 2
- 231100000719 pollutant Toxicity 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- TUJKJAMUKRIRHC-UHFFFAOYSA-N hydroxyl Chemical compound [OH] TUJKJAMUKRIRHC-UHFFFAOYSA-N 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 230000002503 metabolic effect Effects 0.000 description 1
- 230000000813 microbial effect Effects 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 125000001997 phenyl group Chemical group [H]C1=C([H])C([H])=C(*)C([H])=C1[H] 0.000 description 1
- 230000035755 proliferation Effects 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 238000007142 ring opening reaction Methods 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 230000001954 sterilising effect Effects 0.000 description 1
- 239000006228 supernatant Substances 0.000 description 1
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- Treatment Of Water By Oxidation Or Reduction (AREA)
Abstract
The biochemical and ozone oxidation coupling reactor device of the utility model comprises: the device comprises a shell, a first elastic filler, a first aeration pipe, an ozone oxidation filler, a second elastic filler, a tail gas collecting pipe, an ozone generator, an ozone tail gas processor, a second aeration pipe, a third aeration pipe, a baffle plate and a filler frame, wherein a water inlet pipe is arranged at the upper end of the side wall of a microorganism adsorption zone, the first elastic filler is arranged in the filler frame, and the first aeration pipe is arranged at the lower end of the microorganism adsorption zone below the filler frame; the filler frame is internally filled with ozone oxidation filler, and the second aeration pipe is arranged at the lower end of the ozone oxidation area below the filler frame; the second elastic filler is arranged in the filler frame, the third aeration pipe is arranged at the lower end of the microorganism metabolism area below the filler frame, the ozone generator arranged outside the shell is connected with the second aeration pipe through a pipeline, the tail gas collecting pipe is arranged at the upper end of the ozone oxidation area, and the tail gas collecting pipe is respectively connected with the first aeration pipe, the ozone tail gas processor and the second aeration pipe through pipelines.
Description
Technical Field
The utility model relates to the field of advanced treatment of industrial wastewater, in particular to a biochemical and ozone oxidation coupling reactor device.
Background
Ozone oxidation is a relatively popular method in advanced treatment of industrial wastewater. The hydroxyl radical generated by the ozone oxidation reaction is used for strongly oxidizing the organic matters which are difficult to biodegrade in the wastewater. The ozone oxidation treatment is mainly carried out after the biochemical reaction of the wastewater, and macromolecular organic matters containing degradation such as benzene rings and the like in the biochemical treatment can be degraded and subjected to ring opening in the ozone oxidation stage, so that the COD of the wastewater is further reduced, and the biodegradability in the wastewater is regulated. Ozone oxidation also has the functions of decoloring and sterilizing in the process of removing refractory organic matters. Ozone oxidation is often used with a catalyst, which can significantly improve the efficiency of ozone oxidation.
The main disadvantage of the existing ozone oxidation process is that the energy consumption is relatively high, and the investment of the whole process is relatively large. The ozone oxidation residence time of the monomer adopting the ozone oxidation process is 0.5-1 hour in the COD removal process, wherein the catalyst bed residence time is 15 minutes. Ozone adding amount is 50-100mg/L, running cost is 0.7-1.4 yuan/ton of water (electricity fee and liquid oxygen fee), investment intensity is 0.04 yuan/ton of water, and occupied area is 0.06m 2 Per ton of water.
Disclosure of Invention
The utility model aims to provide a biochemical and ozone oxidation coupling reactor device, which can greatly reduce the energy consumption for removing COD by ozone oxidation alone and greatly reduce the investment cost of ozone oxidized monomers by utilizing the combined technology of ozone and biochemical technology. Under the condition that the original COD removal load is unchanged, the energy consumption per unit COD removal load is reduced, and the investment per unit COD removal load is reduced.
In order to achieve the aim of the utility model, the utility model adopts the following technical scheme:
the utility model relates to a biochemical and ozone oxidation coupling reactor device, which comprises: the device comprises a shell, a first elastic filler, a first aeration pipe, an ozone oxidation filler, a second elastic filler, a tail gas collecting pipe, an ozone generator, an ozone tail gas processor, a second aeration pipe, a third aeration pipe, a partition board and a filler frame, wherein the shell is a cuboid, the partition board sequentially separates the cuboid into a microorganism adsorption area, an ozone oxidation area and a microorganism metabolism area which are arranged in a line, a water inlet pipe is arranged at the upper end of the side wall of the microorganism adsorption area, a filler frame is arranged in the middle of the microorganism adsorption area, the first elastic filler is arranged in the filler frame, the first aeration pipe is arranged at the lower end of the microorganism adsorption area below the filler frame, and a lower water passing port is arranged at the lower end of the partition board between the microorganism adsorption area and the ozone oxidation area; a filler frame is arranged in the middle of the ozone oxidation zone, ozone oxidation filler is arranged in the filler frame, a second aeration pipe is arranged at the lower end of the ozone oxidation zone below the filler frame, and an upper water passing port is arranged at the upper end of a partition plate between the ozone oxidation zone and the microorganism metabolism zone; a filling frame is arranged in the middle of the microorganism metabolism area, a second elastic filler is arranged in the filling frame, a third aeration pipe is arranged at the lower end of the microorganism metabolism area below the filling frame, and a drain pipe is arranged at the lower end of the side wall of the microorganism metabolism area, wherein: the ozone generator outside the casing is connected with the second aeration pipe through a pipeline, the upper end of the ozone oxidation area is provided with a tail gas collecting pipe, and the tail gas collecting pipe is respectively connected with the first aeration pipe, the ozone tail gas processor and the third aeration pipe through pipelines.
The utility model relates to a biochemical and ozone oxidation coupling reactor device, wherein: two-way valves are respectively arranged on the pipelines which are communicated with the first aeration pipe and the third aeration pipe.
The utility model relates to a biochemical and ozone oxidation coupling reactor device, wherein: a plurality of ropes are fixed on the filling frames of the microorganism adsorption area and the microorganism metabolism area, and a plurality of first elastic fillers or second elastic fillers are tied on each rope.
The utility model relates to a biochemical and ozone oxidation coupling reactor device, wherein: the ropes are fixed on the upper frame and the lower frame of the packing frame or on the left frame and the right frame of the packing frame.
The utility model relates to a biochemical and ozone oxidation coupling reactor device, wherein: the ozonated filler is stacked in a filler frame of the ozonation zone.
The utility model has the innovation point that the biochemical treatment technology and the ozone oxidation technology are organically combined together. After the proliferation of microorganisms on the first elastic filler in the microorganism adsorption zone reaches a certain amount, the microorganism adsorption zone can adsorb pollutants such as COD in the wastewater, so that a part of refractory substances such as COD can be reduced. The wastewater after microorganism adsorption flows into the ozone oxidation zone, and part of COD is reduced in the microorganism adsorption zone, so that the concentration of ozone supplied to the ozone oxidation zone can be lower, and the amount of catalyst put in is smaller. After the ozone oxidation, macromolecular organic matters in the wastewater are strongly oxidized into micromolecular organic matters, so that the biodegradability in the wastewater is changed. Meanwhile, after the refractory substances in the wastewater are oxidized, COD in the wastewater is further removed. Part of ozone tail gas generated in the ozone oxidation area is removed by the tail gas treatment device, and the other part of the ozone tail gas is recycled for oxygen supply in the microorganism adsorption area and the microorganism metabolism area. The wastewater after ozone oxidation flows into a microorganism metabolism area, a second elastic filler is arranged in the microorganism metabolism area, microorganisms in the wastewater hang on the surface of the second elastic filler when flowing through the microorganism metabolism area, and the microorganisms are continuously domesticated and added. The wastewater flowing from the ozone oxidation zone undergoes biochemical reactions in the microorganism metabolism zone. After the micromolecular organic matters generated after the ozone reaction are decomposed and metabolized by microorganisms, COD in the wastewater can be further reduced. The biochemical treatment and ozone combined treatment mode is adopted, and the operation cost and the investment cost are greatly reduced.
The utility model utilizes the adsorption and degradation of pollutants in wastewater by biochemical reaction, reduces the ozone adding concentration of an ozone oxidation area and reduces the use amount of an ozone catalyst. The reduction of the ozone adding concentration can reduce the power of the ozone generator and greatly reduce the running electricity cost. The reduction of the catalyst brings about a reduction of investment costs. The utility model creatively uses the ozone tail gas recycling system, and recycles part of the generated ozone tail gas as a part of the oxygen supply system. The energy consumption of the whole process equipment is reduced to the maximum extent. The redundant ozone tail gas is broken by utilizing a tail gas treatment device.
Drawings
FIG. 1 is a schematic view of a forward section of a biochemical and ozone oxidation reactor device according to the present utility model;
FIG. 2 is a graph showing a comparison of ozone concentration in an ozone reactor at the same COD load removed;
FIG. 3 is a graph comparing the energy consumption of an ozone reactor with the same COD load removed.
In fig. 1, reference numeral 1 denotes a water inlet pipe; reference numeral 2 denotes a first elastic filler; reference numeral 3 is a first aerator pipe; reference numeral 4 is a lower water passing port; reference numeral 5 denotes an ozone oxidized filler; reference numeral 6 is a drain pipe; reference numeral 7 denotes a second elastic filler; reference numeral 8 is an upper water passing port; reference numeral 9 is a tail gas collecting pipe; reference numeral 10 is an ozone generator; reference numeral 11 is an ozone tail gas processor; reference numeral 12 denotes a second aerator pipe; reference numeral 13 denotes a third aerator pipe; reference numeral 14 is a separator; reference numeral 15 denotes a filler frame; reference numeral 16 denotes a microorganism adsorbing region; reference numeral 17 denotes an ozone oxidation zone; reference numeral 18 denotes a microorganism metabolic region; reference numeral 19 is a two-way valve; reference numeral 20 is a housing; reference numeral 21 denotes a rope.
Detailed Description
The present utility model will be described in detail with reference to the accompanying drawings.
Detailed exemplary embodiments are disclosed below. However, specific structural and functional details disclosed herein are merely for purposes of describing example embodiments.
As shown in fig. 1, the biochemical and ozone oxidation coupling reactor device of the present utility model comprises: the device comprises a shell 20, a first elastic filler 2, a first aerator pipe 3, an ozone oxidation filler 5, a second elastic filler 7, a tail gas collecting pipe 9, an ozone generator 10, an ozone tail gas processor 11, a second aerator pipe 12, a third aerator pipe 13, a partition board 14 and a filler frame 15, wherein the shell 20 is a cuboid, the partition board 14 sequentially divides the cuboid into a microorganism adsorption area 16, an ozone oxidation area 17 and a microorganism metabolism area 18 which are arranged in a straight line, the water inlet pipe 1 is arranged at the upper end of the side wall of the microorganism adsorption area 16, the filler frame 15 is arranged in the middle of the microorganism adsorption area 16, the first elastic filler 2 is arranged in the filler frame 15, the first aerator pipe 3 is arranged at the lower end of the microorganism adsorption area 16 below the filler frame 15, and a water outlet 4 is arranged at the lower end of the partition board 14 between the microorganism adsorption area 16 and the ozone oxidation area 17; a filler frame 15 is arranged in the middle of the ozone oxidation zone 17, ozone oxidation filler 5 is arranged in the filler frame 15, a second aerator pipe 12 is arranged at the lower end of the ozone oxidation zone 17 below the filler frame 15, and an upper water outlet 8 is arranged at the upper end of a partition plate 14 between the ozone oxidation zone 17 and a microorganism metabolism zone 18; a filler frame 15 is arranged in the middle of a microorganism metabolism area 18, a second elastic filler 7 is arranged in the filler frame 15, a third aerator pipe 13 is arranged at the lower end of the microorganism metabolism area 18 below the filler frame 15, a drain pipe 6 is arranged at the lower end of the side wall of the microorganism metabolism area 18, an ozone generator 10 arranged outside a shell 20 is connected with the second aerator pipe 12 through a pipeline, a tail gas collecting pipe 9 is arranged at the upper end of the ozone oxidation area 17, the tail gas collecting pipe 9 is respectively connected with the first aerator pipe 3, an ozone tail gas processor 11 and the third aerator pipe 13 through pipelines, and two-way valves 19 are respectively arranged on the pipelines leading in the first aerator pipe 3 and the third aerator pipe 13.
A plurality of ropes 21 are fixed on the packing boxes 15 of the microorganism adsorption zone 16 and the microorganism metabolism zone 18, and a plurality of first elastic packing 2 or second elastic packing 7 are tied on each rope 21. The ropes 21 are fixed to the upper and lower rims of the packing frame 15 or to the left and right rims of the packing frame 15. The ozonated packing 5 is stacked in a packing frame 15 of an ozonation zone 17.
The utility model is arranged at the rear end of biochemical treatment of industrial wastewater, and after the biochemical treatment of the industrial wastewater, the microorganisms degrade the easily biodegradable organic matters in the wastewater. After the wastewater passes through the sedimentation tank, the supernatant enters a biochemical-ozone oxidation coupling reactor. The inflow water flows into a microorganism adsorption zone 16 after passing through the water inlet pipe 1, a biological film is formed on the surface of the first elastic filler 2, oxygen is provided by ozone tail gas through the first aeration pipe 3 in the microorganism adsorption zone, then wastewater flows into an ozone oxidation zone 17 through the sewage outlet 4, ozone generated by the ozone generator 10 is aerated through the second aeration pipe 12, reaction is carried out under the action of an ozone catalyst, and the generated tail gas is discharged into the ozone tail gas processor 11 for treatment. The wastewater flows into a microorganism metabolism area 18 through the upper water outlet 8, a biological film is formed on the surface of the second elastic filler 7, then biochemical reaction is carried out, ozone tail gas is subjected to rectangular aeration through the third aeration pipe 13, and finally the wastewater is discharged from the discharge pipe 6.
A method of using the biochemical and ozone oxidation coupled reactor apparatus shown in fig. 1, wherein: it comprises the following steps:
(A) The biochemical tail water of the industrial wastewater flows into a microorganism adsorption area 16, a film is hung on the first elastic filler 2, and the first aerator pipe 3 provides oxygen for microorganism growth; the grown microbial film absorbs a part of refractory organic matters in the biochemical tail water.
(B) The biochemical tail water flows into the ozone oxidation area, flows through the ozone and the catalyst filler 5 from bottom to top, and simultaneously undergoes ozone oxidation reaction under the action of the second aerator pipe 12, and the effluent flows through the water gap 8 to the microorganism metabolism area 18.
(C) And the biochemical tail water is subjected to film formation on the second elastic filler 7, and microorganisms grow on the surface of the second elastic filler 7 to form a biological film. After the wastewater is subjected to an ozone oxidation process reaction, macromolecular organic matters are converted into micromolecular organic matters, microorganisms in the biological film metabolize the micromolecular organic matters in the wastewater, and finally effluent water is discharged from the discharge pipe 6.
As shown in FIG. 2, the biochemical and ozone oxidation coupled reactor of the present utility model was compared with a conventional ozone oxidation reactor to remove 1g of COD, and the quality of ozone required in the reactor was evaluated. The biochemical tail water with COD of 500mg/L is respectively introduced into 2 reactors with the same volume for reaction for 30min, and the COD concentration in the water is detected. It is calculated that the conventional ozone oxidation process requires 4g of ozone for removing 1g of COD, whereas the coupled biochemical and ozone oxidation reactor requires only 1g of ozone for removing 1g of COD. The biochemical and ozone oxidation coupling reactor has lower ozone usage and thus lower ozone generation than the traditional ozone oxidation reactor.
As shown in FIG. 3, the biochemical and ozone oxidation coupled reactor of the present utility model was compared with a conventional ozone oxidation reactor to remove the electricity required to be consumed in the reactor at 1g COD as a judgment. The biochemical tail water with COD of 500mg/L is respectively introduced into 2 reactors with the same volume for reaction for 30min, and the COD concentration and the power consumption in the water are detected. It is calculated that the conventional ozone oxidation process consumes 60kwh for removing 1 gcos, whereas the coupled biochemical and ozone oxidation reactor consumes only 40kwh for removing 1 gcos. The biochemical and ozone oxidation coupling reactor has lower energy consumption than the traditional ozone oxidation reactor.
It is to be understood that the above-described embodiments of the present utility model are merely illustrative of or explanation of the principles of the present utility model and are in no way limiting of the utility model. Accordingly, any modification, equivalent replacement, improvement, etc. made without departing from the spirit and scope of the present utility model should be included in the scope of the present utility model. Furthermore, the appended claims are intended to cover all such changes and modifications that fall within the scope and boundary of the appended claims, or equivalents of such scope and boundary.
Claims (5)
1. A biochemical and ozone oxidation coupled reactor device comprising: the device comprises a shell (20), a first elastic filler (2), a first aerator pipe (3), an ozone oxidation filler (5), a second elastic filler (7), a tail gas collecting pipe (9), an ozone generator (10), an ozone tail gas processor (11), a second aerator pipe (12), a third aerator pipe (13), a partition board (14) and a filler frame (15), wherein the shell (20) is a cuboid, the partition board (14) sequentially partitions the cuboid into a microbe adsorption area (16), an ozone oxidation area (17) and a microbe metabolism area (18) which are arranged in a row, a water inlet pipe (1) is arranged at the upper end of the side wall of the microbe adsorption area (16), a filler frame (15) is arranged in the middle of the microbe adsorption area (16), the first elastic filler (2) is arranged in the filler frame (15), the first aerator pipe (3) is arranged at the lower end of the microbe adsorption area (16) below the filler frame (15), and a water outlet (4) is arranged at the lower end of the partition board (14) between the microbe adsorption area (16) and the ozone oxidation area (17); a filler frame (15) is arranged in the middle of the ozone oxidation zone (17), ozone oxidation filler (5) is arranged in the filler frame (15), a second aerator pipe (12) is arranged at the lower end of the ozone oxidation zone (17) below the filler frame (15), and an upper water outlet (8) is arranged at the upper end of a partition plate (14) between the ozone oxidation zone (17) and a microorganism metabolism zone (18); a filling frame (15) is arranged in the middle of a microorganism metabolism area (18), a second elastic filler (7) is arranged in the filling frame (15), a third aerator pipe (13) is arranged at the lower end of the microorganism metabolism area (18) below the filling frame (15), and a drain pipe (6) is arranged at the lower end of the side wall of the microorganism metabolism area (18), and is characterized in that: an ozone generator (10) arranged outside the shell (20) is connected with a second aerator pipe (12) through a pipeline, a tail gas collecting pipe (9) is arranged at the upper end of the ozone oxidation area (17), and the tail gas collecting pipe (9) is respectively connected with the first aerator pipe (3), an ozone tail gas processor (11) and a third aerator pipe (13) through pipelines.
2. The biochemical and ozone oxidation coupled reactor device according to claim 1, wherein: two-way valves (19) are respectively arranged on the pipelines which are communicated with the first aeration pipe (3) and the third aeration pipe (13).
3. The biochemical and ozone oxidation coupled reactor device according to claim 2, wherein: a plurality of ropes (21) are fixed on a packing frame (15) of the microorganism adsorption area (16) and the microorganism metabolism area (18), and a plurality of first elastic packing (2) or second elastic packing (7) are tied on each rope (21).
4. A biochemical and ozonation coupling reactor apparatus according to claim 3, wherein: the ropes (21) are fixed on the upper frame and the lower frame of the packing frame (15) or on the left frame and the right frame of the packing frame (15).
5. The biochemical and ozone oxidation coupled reactor device according to claim 4, wherein: the ozonated filler (5) is stacked in a filler frame (15) of an ozonation zone (17).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321468461.2U CN220012315U (en) | 2023-06-09 | 2023-06-09 | Biochemical and ozone oxidation coupling reactor device |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321468461.2U CN220012315U (en) | 2023-06-09 | 2023-06-09 | Biochemical and ozone oxidation coupling reactor device |
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| Publication Number | Publication Date |
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| CN220012315U true CN220012315U (en) | 2023-11-14 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN202321468461.2U Active CN220012315U (en) | 2023-06-09 | 2023-06-09 | Biochemical and ozone oxidation coupling reactor device |
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| Country | Link |
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| CN (1) | CN220012315U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116903149A (en) * | 2023-06-09 | 2023-10-20 | 德威华泰科技股份有限公司 | Method for treating biochemical tail water by using biochemical and ozone oxidation coupling reactor device |
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2023
- 2023-06-09 CN CN202321468461.2U patent/CN220012315U/en active Active
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116903149A (en) * | 2023-06-09 | 2023-10-20 | 德威华泰科技股份有限公司 | Method for treating biochemical tail water by using biochemical and ozone oxidation coupling reactor device |
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